US4428829A - Process for simultaneous separation of aromatics from heavy and light hydrocarbon streams - Google Patents

Process for simultaneous separation of aromatics from heavy and light hydrocarbon streams Download PDF

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Publication number
US4428829A
US4428829A US06/301,493 US30149381A US4428829A US 4428829 A US4428829 A US 4428829A US 30149381 A US30149381 A US 30149381A US 4428829 A US4428829 A US 4428829A
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United States
Prior art keywords
aromatics
extractor
selective solvent
hydrocarbon stream
light
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Expired - Fee Related
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US06/301,493
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English (en)
Inventor
Walter C. G. Kosters
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Shell USA Inc
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Shell Oil Co
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Assigned to SHELL OIL COMPANY reassignment SHELL OIL COMPANY ASSIGNMENT OF ASSIGNORS INTEREST. Assignors: KOSTERS, WALTER C. G.
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents

Definitions

  • the invention relates to a process for the simultaneous separation of aromatics and non-aromatics from a heavy hydrocarbon stream and a light hydrocarbon stream.
  • the invention provides a method in which heavy hydrocarbon streams and light hydrocarbon streams can be separated simultaneously into aromatics and non-aromatics without the need of more complicated separation methods than extraction and distillation.
  • step (g) the selective solvent obtained in step (f) is at least partially recycled to the first extractor.
  • a light hydrocarbon stream in the context of this specification and claims is a hydrocarbon stream which has a boiling range which is lower than the boiling point (or if appropriate boiling range) of the selective solvent used.
  • a heavy hydrocarbon stream in the context of this specification and claims is a hydrocarbon stream which has a boiling range which is higher than that of the light hydrocarbon stream. Although there may be some overlap of the boiling range of the light and the heavy hydrocarbon streams, it is preferred that no such overlap exists.
  • the boiling range of the heavy hydrocarbon stream may be lower or higher than or comprises the boiling point (or if appropriate boiling range) of the selective solvent used.
  • Light hydrocarbon streams which boil in the range from 50°-170° C., such as gasoline fractions, which may be straight run or have been obtained from a conversion process, in particular from catalytic reforming or from a pyrolysis process, are preferred.
  • Very suitable heavy hydrocarbon streams are boiling in the range from 150°-350° C., such as kerosines, gas oils, which may have been obtained as straight run fractions or from a catalytic or non-catalytic process e.g., thermal cracking, catalytic cracking and/or hydrocracking.
  • solvents which at least in part are of the sulfolane, the glycol, the morpholine and/or the pyrrolidone/piperidone type; i.e., sulfolane (cyclic tetramethylene sulphone), the unsaturated analogues thereof and the derivatives of both, as described, for example, in U.K. Patent Specification No.
  • the selective solvent may contain a quantity of a substance, such as water, which has a favourable effect on the selectivity and/or the solvent power thereof.
  • a selective solvent which totally or substantially consists of sulfolane is in particular preferred.
  • the extractions in the first and second extractor are preferably carried out in multistage; use may be made of any suitable equipment.
  • the extractions may e.g., be carried out with the aid of a number of mixing and settling steps. It is preferred to carry out the extractions by means of an extraction column, in particular a rotating disc contactor such as described e.g. in U.K. patent specification No. 659,241.
  • the raffinates from the first and second extractor contain a small amount of the selective solvent which is to be removed. It is preferred to wash these raffinates with water in order to remove the selective solvent therefrom.
  • the extract phase from the first extractor which contains aromatics extracted from the heavy hydrocarbon stream (also indicated as heavy aromatics) is used as the extracting solvent for the light hydro-carbon stream in the second extractor.
  • a raffinate is obtained which comprises all or the greater part of the heavy aromatics and the non-aromatics extracted from the light hydrocarbon stream (also indicated as light non-aromatics) together with a small amount of selective solvent; the extract phase containing all or the greater part of the aromatics extracted from the light hydrocarbon stream (also indicated as light aromatics).
  • the raffinate can (after having been washed with water) if desired be easily separated in light non-aromatics and heavy aromatics by distillation because of the difference in boiling ranges between these fractions.
  • the extract phase from the second extractor which contains light aromatics and part of the light non-aromatics is subjected to extractive distillation in order to remove the light non-aromatics therefrom.
  • hydrocarbons at least partially in the vapour phase are contacted with liquid selective solvent, as a result of which aromatics are separated from non-aromatics, the latter being removed in the vapour form.
  • the overhead fraction of the extractive distillation which contains light non-aromatics and a small amount of light aromatics is very suitably condensed, the water layer (if any) is removed, and the hydrocarbon layer is recirculated to the second extractor.
  • the greater part of the light aromatics remains in the bottom fraction of the extractive distillation. According to the invention these light aromatics are separated from the selective solvent by distillation of the bottom fraction of the extractive distillation.
  • This distillation is very conveniently carried out in a separate column, very suitably under reduced pressure.
  • Preferably steam is introduced to improve the separation.
  • the overhead product which contains steam and light aromatics is cooled, the water layer is separated and the light aromatics (which may be partially recycled to the distillation column) are removed.
  • the amount of fresh water to be introduced into the system can be kept limited by reintroduction into the system of at least part of the aqueous liquids becoming available from the water-washes of the raffinates of the extractors, from the top product of the distillation in which the selective solvent is separated from the light aromatics. It is in particular attractive to use at least part of the water phase obtained as top product of the distillation in which the selective solvent is separated from the light aromatics as washing medium for the raffinates.
  • the selective solvent obtained after removal of the light aromatics is at least partially recycled to the first extractor. If desired part thereof may be recycled to the second extractor, and may be introduced therein together with the extract phase from the first extractor and/or at a point nearer to the entrance of the light hydrocarbon stream into the second extractor. If desired, part of the selective solvent may also be introduced into the extractive distillation column.
  • a heavy hydrocarbon stream is introduced via line 1 into the first extractor 2, into which first extractor selective solvent is introduced via line 3.
  • Raffinate is leaving extractor 2 via line 4, and is water-washed (not shown).
  • the extract phase is removed via line 5 and introduced into the second extractor 6.
  • a light hydrocarbon stream is introduced into extractor 6 via line 7.
  • selective solvent is introduced into extractor 6 via line 8.
  • the raffinate which leaves extractor 6 via line 9 is water-washed (not shown) and is distilled (not shown) to yield heavy aromatics and light non-aromatics.
  • the extract phase is leaving extractor 6 via line 10 and is led via heat-exchanger 11 to extractive distillation column 12.
  • the top product thereof is forwarded to a separation vessel 26 via line 13.
  • 61 t/d of a kerosine fraction with a boiling range of 190°-240° C., which contains 20% w aromatics is fed to extractor 2 via line 1.
  • the extractor is a rotating disc contactor of the type described in British patent specification No. 659,241.
  • the extraction is carried out at a temperature of 125° C. with sulfolane forwarded via line 3 in an amount of 555 t/d.
  • the raffinate leaving the extractor via line 4 is washed with water yielding 37 t/d of heavy non-aromatics (the aromatics content is below 1% w).
  • extractor 6 (which is also a rotating disc contactor) there are fed via line 7 122 t/d of a light straight run hydrocarbon fraction with a boiling range of 55°-85° C. which contains 5% w benzene.
  • the extract phase from extractor 2 (579 t/d) is introduced into extractor 6 via line 5.
  • the temperature in extractor 6 is 90° C.
  • Via line 8 430 t/d sulfolane is also introduced into extractor 6.
  • the raffinate phase leaving the extractor via line 9 is washed with water yielding 134 t/d raffinate.
  • the extract phase of extractor 6 (1025 t/d) is fed (after being heat-exchanged in heatexchanger 11) to extractive distillation column 12 via line 10.
  • the extractive distillation in column 12 is carried out at a pressure of 0.2 bar and a bottom temperature of 175° C.
  • the overhead product is forwarded via line 13 to separator 26 and separated in a water phase and a hydrocarbon phase; the hydrocarbon phase is recycled to extractor 6 via line 14.
  • the bottom product of column 12 is fed via line 16 to distillation column 17 which is heated with steam from line 18.
  • the top product is led via line 19 to separator 20, the hydrocarbon phase (light aromatics) obtained therein partly recycled to the distillation column via line 21, and partly removed via line 22 in the amount of 12 t/d.
  • the raffinate emerging via line 9 from extractor 6 (which contains less than 100 ppm benzene) is water washed and distilled yielding 24 t/d heavy aromatics and 110 t/d food-grade hexane.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
US06/301,493 1980-10-16 1981-09-14 Process for simultaneous separation of aromatics from heavy and light hydrocarbon streams Expired - Fee Related US4428829A (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GB8033462 1980-10-16
GB8033462 1980-10-16

Publications (1)

Publication Number Publication Date
US4428829A true US4428829A (en) 1984-01-31

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US06/301,493 Expired - Fee Related US4428829A (en) 1980-10-16 1981-09-14 Process for simultaneous separation of aromatics from heavy and light hydrocarbon streams

Country Status (10)

Country Link
US (1) US4428829A (de)
EP (1) EP0050381B1 (de)
JP (1) JPS5794090A (de)
AU (1) AU543480B2 (de)
CA (1) CA1169012A (de)
DE (1) DE3165088D1 (de)
MY (1) MY8500924A (de)
SG (1) SG68384G (de)
SU (1) SU1122217A3 (de)
ZA (1) ZA817093B (de)

Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5039399A (en) * 1989-11-20 1991-08-13 Texaco Inc. Solvent extraction of lubricating oils
US5041206A (en) * 1989-11-20 1991-08-20 Texaco Inc. Solvent extraction of lubricating oils
US5186817A (en) * 1986-09-12 1993-02-16 The Standard Oil Company Process for separating extractable organic material from compositions comprising oil-in-water emulsions comprising said extractable organic material and solids
US20080167511A1 (en) * 2007-01-10 2008-07-10 Holloman Corporation Carbon Dioxide Fractionalization Process
US8455709B2 (en) 2008-12-09 2013-06-04 Gtc Technology Us, Llc Heavy hydrocarbon removal systems and methods
WO2013136169A1 (en) 2012-03-16 2013-09-19 Bharat Petroleum Corporation Limited Process for obtaining food grade hexane
US9144753B2 (en) 2011-07-29 2015-09-29 Saudi Arabian Oil Company Selective series-flow hydroprocessing system and method
US9145521B2 (en) 2011-07-29 2015-09-29 Saudi Arabian Oil Company Selective two-stage hydroprocessing system and method
US9144752B2 (en) 2011-07-29 2015-09-29 Saudi Arabian Oil Company Selective two-stage hydroprocessing system and method
US9359566B2 (en) 2011-07-29 2016-06-07 Saudi Arabian Oil Company Selective single-stage hydroprocessing system and method
US9556388B2 (en) 2011-07-29 2017-01-31 Saudi Arabian Oil Company Selective series-flow hydroprocessing system and method
US10702795B2 (en) 2016-01-18 2020-07-07 Indian Oil Corporation Limited Process for high purity hexane and production thereof

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2666729C1 (ru) * 2017-12-28 2018-09-12 Публичное акционерное общество "Татнефть" имени В.Д. Шашина Способ очистки тяжелого нефтяного сырья от неорганических примесей

Family Cites Families (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
NL40626C (de) * 1934-07-14
BE509744A (de) * 1951-03-05
US2886523A (en) * 1955-04-25 1959-05-12 Shell Dev Lubricating oil refining process
US3202990A (en) * 1959-05-04 1965-08-24 Gen Electric Intermediate frequency side-lobe canceller
NL137161C (de) * 1961-09-21
US3725922A (en) * 1971-09-13 1973-04-03 Technology Service Corp Convergence rate improvement for adaptive receiving array antennas of higher order than 2-pulse mti cancellers
US3727220A (en) * 1971-09-13 1973-04-10 Technology Service Corp Adaptive receiving array method and apparatus for mti radar
US3982245A (en) * 1974-07-15 1976-09-21 General Electric Company Sidelobe canceller with programmable correlation signal weighting
US3995271A (en) * 1975-08-20 1976-11-30 The United States Of America As Represented By The Secretary Of The Air Force Adaptive clutter cancellation and interference rejection system for AMTI radar
US4035799A (en) * 1975-11-04 1977-07-12 The United States Of America As Represented By The Secretary Of The Navy Digital mean clutter doppler compensation system
US4086592A (en) * 1977-07-22 1978-04-25 The United States Of America As Represented By The Secretary Of The Navy Digital sidelobe canceller
US4222051A (en) * 1979-01-18 1980-09-09 The United States Of America As Represented By The Secretary Of The Navy Cascaded digital cancelers

Cited By (20)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5186817A (en) * 1986-09-12 1993-02-16 The Standard Oil Company Process for separating extractable organic material from compositions comprising oil-in-water emulsions comprising said extractable organic material and solids
US5039399A (en) * 1989-11-20 1991-08-13 Texaco Inc. Solvent extraction of lubricating oils
US5041206A (en) * 1989-11-20 1991-08-20 Texaco Inc. Solvent extraction of lubricating oils
US8709215B2 (en) 2007-01-10 2014-04-29 Pilot Energy Solutions, Llc Carbon dioxide fractionalization process
US9481834B2 (en) 2007-01-10 2016-11-01 Pilot Energy Solutions, Llc Carbon dioxide fractionalization process
US7777088B2 (en) 2007-01-10 2010-08-17 Pilot Energy Solutions, Llc Carbon dioxide fractionalization process
US20100258401A1 (en) * 2007-01-10 2010-10-14 Pilot Energy Solutions, Llc Carbon Dioxide Fractionalization Process
US10316260B2 (en) 2007-01-10 2019-06-11 Pilot Energy Solutions, Llc Carbon dioxide fractionalization process
USRE44462E1 (en) 2007-01-10 2013-08-27 Pilot Energy Solutions, Llc Carbon dioxide fractionalization process
WO2008086265A1 (en) * 2007-01-10 2008-07-17 Holloman Corporation Carbon dioxide fractionalization process
US20080167511A1 (en) * 2007-01-10 2008-07-10 Holloman Corporation Carbon Dioxide Fractionalization Process
US9370728B2 (en) 2008-12-09 2016-06-21 Gtc Technology Us Llc Heavy hydrocarbon removal systems and methods
US8455709B2 (en) 2008-12-09 2013-06-04 Gtc Technology Us, Llc Heavy hydrocarbon removal systems and methods
US9144753B2 (en) 2011-07-29 2015-09-29 Saudi Arabian Oil Company Selective series-flow hydroprocessing system and method
US9145521B2 (en) 2011-07-29 2015-09-29 Saudi Arabian Oil Company Selective two-stage hydroprocessing system and method
US9144752B2 (en) 2011-07-29 2015-09-29 Saudi Arabian Oil Company Selective two-stage hydroprocessing system and method
US9359566B2 (en) 2011-07-29 2016-06-07 Saudi Arabian Oil Company Selective single-stage hydroprocessing system and method
US9556388B2 (en) 2011-07-29 2017-01-31 Saudi Arabian Oil Company Selective series-flow hydroprocessing system and method
WO2013136169A1 (en) 2012-03-16 2013-09-19 Bharat Petroleum Corporation Limited Process for obtaining food grade hexane
US10702795B2 (en) 2016-01-18 2020-07-07 Indian Oil Corporation Limited Process for high purity hexane and production thereof

Also Published As

Publication number Publication date
JPH0257595B2 (de) 1990-12-05
EP0050381B1 (de) 1984-07-25
SU1122217A3 (ru) 1984-10-30
AU543480B2 (en) 1985-04-18
ZA817093B (en) 1982-09-29
AU7631681A (en) 1982-04-22
JPS5794090A (en) 1982-06-11
DE3165088D1 (en) 1984-08-30
MY8500924A (en) 1985-12-31
CA1169012A (en) 1984-06-12
SG68384G (en) 1985-06-14
EP0050381A1 (de) 1982-04-28

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